Process for producing polycrystalline silicon

ABSTRACT

Deposition on a sightglass in a reactor for CVD deposition of silicon is reduced by conducting a first purge gas stream substantially parallel to the reactor end surface of the sightglass, and conducting a second purge gas stream within the sightglass tube at an angle from the sightglass surface toward the interior of the reactor.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application is a division of U.S. application Ser. No. 14/907,932filed Jan. 27, 2016, now pending, which is the U.S. National Phase ofPCT Appln. No. PCT/EP2014/064851 filed Jul. 10, 2014, which claimspriority to German Application No. 10 2013 214 799.6 filed Jul. 29,2013, the disclosures of which are incorporated in their entirety byreference herein.

BACKGROUND OF THE INVENTION 1. Field of the Invention

The invention provides a process for producing polycrystalline silicon.

2. Description of the Related Art

Polycrystalline silicon (polysilicon for short) serves as a startingmaterial in the production of monocrystalline silicon by means ofcrucible pulling (Czochralski or CZ process) or by means of zone melting(float zone or FZ process). This monocrystalline silicon is divided intowafers and, after a multitude of mechanical, chemical andchemo-mechanical processing operations, used in the semiconductorindustry for manufacture of electronic components (chips).

More particularly, however, polycrystalline silicon is required to anincreased degree for production of mono- or multicrystalline silicon bymeans of pulling or casting processes, this mono- or multicrystallinesilicon serving for manufacture of solar cells for photovoltaics.

The polycrystalline silicon is typically produced by means of theSiemens process. In this process, in a bell jar-shaped reactor (“Siemensreactor”), thin filament rods (“thin rods”) of silicon are heated bydirect passage of current and a reaction gas containing asilicon-containing component and hydrogen is introduced.

The silicon-containing component of the reaction gas is generallymonosilane or a halosilane of the general composition SiH_(n)X_(4-n)(n=0, 1, 2, 3; X═Cl, Br, I). It is preferably a chlorosilane orchlorosilane mixture, more preferably trichlorosilane. PredominantlySiH₄ or SiHCl₃ (trichlorosilane, TCS) is used in a mixture withhydrogen.

EP 2 077 252 A2 describes the typical setup of a reactor type used inthe production of polysilicon.

The reactor base is provided with electrodes that accommodate the thinrods on which silicon is deposited during the growth process, and whichthus grow to form the desired rods of polysilicon. Typically, two thinrods in each case are joined by a bridge to form a pair of thin rods,which form a circuit through the electrodes and through externaldevices, which serves to heat the rod pairs to a particular temperature.

Moreover, the reactor base is additionally provided with nozzles thatsupply the reactor with fresh gas. The offgas is conducted back out ofthe reaction space via orifices.

The amount of reaction gases supplied is typically varied as a functionof the rod diameter, i.e. is generally increased with increasing roddiameter.

High-purity polysilicon is deposited on the heated rods and the bridge,as a result of which the rod diameter grows with time (CVD=chemicalvapor deposition/gas phase deposition).

DE 102 007 047 210 A1 discloses a process that leads to polysilicon rodshaving advantageous flexural strength. Moreover, the specific energyconsumption in this process is particularly low. With regard to processparameters, a maximum value of the flow rate of the chlorosilanesmixture is attained within fewer than 30 hours, preferably within fewerthan 5 hours, with the temperature on the underside of the bridgebetween 1300° C. and 1413° C.

DE 10 2007 023 041 A1 describes a further process for producingpolysilicon, specifically for FZ (float zone) silicon. It envisages arod temperature of 950 to 1090° C. and a particular proportion ofchlorosilanes in the reaction gas up to a rod diameter of 30 mm, and aswitch in the rod temperature to 930 to 1030° C. and an increase in theproportion of chlorosilanes in the reaction gas no later than attainmentof a rod diameter of 120 mm. Abrupt changes in the growth conditionsmust not be made over the entire deposition period.

US 20120048178 A1 discloses a process for producing polycrystallinesilicon, comprising introduction of a reaction gas comprising asilicon-containing component and hydrogen by means of one or morenozzles into a reactor comprising at least one heated filament rod onwhich silicon is deposited, wherein an Archimedes number Ar_(n), whichdescribes flow conditions in the reactor as a function of the fill levelFL which states the ratio of a rod volume to an empty reactor volume inpercent, for a fill level FL of up to 5%, is within a range limited at alower end by a function Ar=2000×FL^(−0.6) and at an upper end by afunction Ar=17000×FL^(−0.9), and at a fill level of greater than 5% iswithin a range from at least 750 to at most 4000.

The fill level of a reactor states the ratio of the volume of the rodsto the empty volume of the reactor in percent. The empty volume of thereactor is constant. The fill level thus increases with increasingprocess duration since the volume of the rods increases.

The Archimedes number is given by

Ar=π*g*L ³ *A _(d)*(T _(rod) −T _(wall))/(2*Q ²*(T _(rod) +T _(wall)))

where g is the acceleration due to gravity in m/s², L is the rod lengthof the filament rods in m, Q is the volume flow of the gas in m³/s underoperating conditions (p, T), A_(d) is the sum total of all the nozzlecross-sectional areas in m², T_(rod) is the rod temperature in K andT_(wall) is the wall temperature in K. The rod temperature is preferably1150K to 1600K. The wall temperature is preferably 300K to 700K.

It is a relatively common observation in the production of thickpolycrystalline silicon rods (having diameter >100 mm) that the rodshave regions with a very rough surface (“popcorn”). These rough regionshave to be separated from the rest of the material and sold at muchlower prices than the rest of the silicon rod.

U.S. Pat. No. 5,904,981 A discloses that a temporary reduction in thetemperature of the rods can reduce the proportion of the popcornmaterial. At the same time, it is disclosed that, proceeding from apolycrystalline silicon rod having a diameter of 5 mm as a filament(thin rod), a surface temperature of the rod is kept at 1030° C. andpolycrystalline silicon is deposited, and, when the rod diameter reaches85 mm, the electrical current is kept constant, as a result of which thetemperature falls, and, as soon as a temperature of 970° C. is attained,the temperature of the rods is increased gradually back up to 1030° C.over a period of 30 hours, stopping the deposition when the rod diameterreaches 120 mm. The proportion of popcorn in this case is 13%. Theeffect of such changes, however, is that the process runs less quicklyand hence the output is reduced, which reduces the economic viability.

In the known processes for deposition of polycrystalline silicon, it isthus necessary to regulate the rod temperature. The temperature at thesurface of the rods is the crucial parameter in the process forproducing polycrystalline silicon, since the polycrystalline silicon isdeposited at the rod surface. For this purpose, the rod temperature hasto be measured. The rod temperature is typically measured with radiationpyrometers on the surfaces of the vertical rods.

Because of its material properties, contactless temperature measurementon silicon is very demanding. This is because the emission level of thematerial varies significantly over the infrared spectrum and isadditionally dependent on the material temperature. In ordernevertheless to achieve exact and repeatable measurement results, themanufacturers provide the instruments with filters to about 0.9 μm, andso evaluate only a small portion of the radiation spectrum, restrictedto a particular wavelength range by a filter, since the emission levelof silicon within this wavelength range is both relatively high andindependent of temperature.

Because of hydrogen in the atmosphere, specific explosion-proof housingsare typically used for the pyrometers.

The pyrometer gains optical access through a sightglass or a window. Thelens or the window for instruments in the near infrared range consistsof glass or quartz glass.

The pyrometers are mounted at the sightglasses outside the reactor andare directed at the polysilicon rod to be measured. The sightglass sealsthe reactor off from the environment by means of a transparent glasssurface and seals.

It has now been found that, in the course of the deposition process, alayer of deposits forms on the sightglass, which may be of differentthickness according to the mode of operation. This particularly affectsthe (inner) glass surface at the reactor end. This layer of depositscauses an attenuation of the measured radiation intensity. As a result,the pyrometer measures temperatures that are too low. The result of thisis that the rod temperatures are set too high by the electrical powerregulation system of the reactor, which causes unwanted processproperties such as dust deposition, impermissibly high popcorn growth,local melting of the silicon rods, etc. In the worst case—namely in thecase of excessively thick deposits—the process has to be endedprematurely.

Economic disadvantages as a result of off-spec and hence reduced-valueproducts or increased production costs as a result of prematurelyshut-down or failed batches are the consequences of deposits on thesightglass.

In the prior art, efforts have been made to minimize formation ofdeposits on the glass surfaces, by blowing an inert gas or hydrogen overthe glass surface, in order to flush silanes or chlorosilanes, whichhave a tendency to form deposits on the glass, away from the glasssurface, or keep them away from the glass surface.

JP2010254561 A2 describes a sightglass where hydrogen is used as purgegas and is injected into the tube. The ratio of tube length to tubediameter (L/D) in this arrangement is between 5 and 10. A disadvantageis the greatly restricted viewing range resulting from the long, thinsightglass tube.

CN 201302372Y likewise discloses a sightglass where particles adheringon the sightglass lens are to be removed by blowing in gas medium(hydrogen) involved in the reaction, which cleans the lens. The innerconnecting tube is connected at one end to a gas medium cleaningapparatus, such that the inside surface of the sightglass lens can becleaned in the course of operation. Between the first sightglass lensand the second sightglass lens is a cooling water duct, by means ofwhich the first sightglass lens and the second sightglass lens can becooled and cleaned.

CN102311120 B discloses a sightglass where hydrogen as purge gas isinjected through a multitude of holes at an oblique angle to thesightglass surface. The holes are distributed over the entirecircumference of the sightglass tube and aligned radially with respectto the axis of the sightglass tube.

However, it has been found that this prevents the formation of depositsonly in some regions of the sightglass, but actually enhances it inother regions. Moreover, it has been observed at times that thepositions of deposit-free regions on the sightglass surface changesduring the process. Thus, reproducible temperature measurements areimpossible.

This problem gave rise to the objective of the invention. The sightglassis to remain free of deposits and impurities over the entire batch run.

SUMMARY OF THE INVENTION

These and other objects are achieved by a process for producingpolycrystalline silicon, comprising introducing a reaction gascomprising a silicon-containing component and hydrogen into a reactorcontaining at least one heated filament rod on which polycrystallinesilicon is deposited, the reactor comprising at least one tubularsightglass secured to an orifice in the reactor wall by a reactor endand having a glass surface at the other end, with supply of a purge gasthrough holes in the sightglass tube during the deposition, wherein onepurge gas stream runs close to the glass surface of the sightglass andessentially parallel to the glass surface and, spaced apart from thispurge gas stream in the direction of the reactor end of the sightglass,at least one further purge gas stream runs at an angle relative to theglass surface in the direction of the reactor end of the sightglass.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 shows, in highly schematic form, a deposition reactor withsightglass.

FIG. 2 shows one embodiment of the invention in longitudinal section.

FIG. 3 shows one embodiment of the invention in cross section throughthe tube.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

The inventors have recognized that, in the solutions proposed in theprior art, it was not possible to reliably prevent contact of thesilicon-containing reaction gas with the glass surface of the sightglassbecause an injector effect was associated with the purge gas jetsdirected toward the glass surface of the sightglass, and this conveyedsilicon-containing reaction gas to the glass surface and led to unwantedformation of deposits at least in some regions.

Therefore, a sightglass having a novel purge gas supply has beendeveloped, which suppresses contact of the glass surfaces on the reactorside with the reaction gas (chlorosilanes) and hence prevents formationof deposits.

In contrast to the prior art, the purge gas is injected here into thesightglass tube at several positions.

A purge gas stream is introduced close to the glass surface of the tube.This runs essentially parallel to the glass surface.

For this purpose, offset rows of holes aligned parallel to the glasssurface are preferably provided in the immediate proximity of the glasssurface. This effectively produces a “curtain” of purge gas that cankeep the reaction gas away from the glass surface.

Without further measures, however, this can only be achieved when thepurge gas rate supplied is suitably selected.

In order to be independent of the purge gas rate supplied, in accordancewith the invention, at least one second purge gas stream is provided,spaced apart from the first purge gas stream in the direction of thereactor end of the tube.

This second purge gas stream does not, or the further purge gas streamsdo not, run parallel to the glass surface of the sightglass, but at anoblique angle, namely inclined with respect to the plane of the glasssurface of the sightglass, specifically in the direction of the reactorend of the sightglass. The reactor end means that end of the tubemounted at an orifice in the reactor wall.

In order to introduce the second purge gas stream into the tube of thesightglass, holes aligned preferably at an oblique angle to the middleof the reactor are present in the tube.

The introduction of the further purge gas stream gives rise to a flowregime independent of the purge gas rate supplied in the sightglasstube.

This enables process-matched regulation of the purge gas rate requiredfor sightglass purging, without worsening the quality of the sightglasspurging.

Suitable purge gas is the following gases or any desired combinations asa gas mixture: noble gases (e.g. Ar, He), nitrogen, chlorosilanes of theSiH_(n)Cl_(n-4) form, n=0-4, in conjunction with a chlorosilane-free gas(e.g. SiCl₄ with hydrogen), hydrogen, HCl gas. Particular preference isgiven to using hydrogen.

LIST OF REFERENCE NUMERALS USED

-   1 deposition reactor-   2 sightglass-   3 glass pane-   4 hole(s) for purge mass flow M1-   5 hole(s) for purge mass flow M2

FIG. 1 shows a deposition reactor 1 and a sightglass 2 secured to thereactor wall.

FIG. 2 shows a deposition reactor 1 and a sightglass 2 secured to thereactor wall and having a glass pane 3. The sightglass 2 comprises tworows of holes 4 for purge mass flow M1 and one row of holes 5 for purgemass flow M2.

FIG. 3 shows section A-A through a row of holes 4 of FIG. 2. It becomesapparent that several holes parallel to one another are present.

The invention enables the use of sightglasses having comparatively smalltube/construction lengths. Thus, preference is given to a ratio L/D oftube length L to tube diameter D of 0.5-4.0. More preferably, the ratioL/D=0.7-3.0, most preferably 1.0-2.0.

Preference is given to injecting a first portion M1 of the purge gasthrough one or more mutually offset rows of holes.

These rows of holes are arranged on one side of the tube, preferably theupper side, within an angle range β1_n (n=index for row of holes) of40°-180°, preferably 50°-130°, more preferably 60°-120°, about thevertical. Rotation of the angle range (β1_n including the holes by0-180° about the tube axis (deviation from the vertical) is possible.

The distance of the holes within a row from the respective neighboringhole may be different or equal within a row, and is preferably equal.

Holes are preferably positioned such that their exit orifices in thesightglass tube are within the angle range β1_n. The rows of holes arepreferably aligned parallel to one another and to the glass surface. Allthe holes are preferably likewise aligned parallel to one another and tothe opposite tube wall. In this way, a broad purge gas curtain is placedin front of the glass surface.

According to the invention, the purge gas is divided into two substreams(M1 and M2). M1 corresponds to the gas stream running parallel to theglass surface, M2 to the gas stream that runs at an oblique angle; seealso FIG. 2. The ratio of the purge mass flow rates is preferably set asfollows: 1/3<M1/M2<20. More preferably, 1<M1/M2<15; most preferably,2<M1/M2<10.

The cross-sectional area of the tube (A_(T)) based on the total area(A_(M1)) of all the holes in the first portion of the purge gas (M1) ispreferably within the range of 8<A_(T)/A_(M1)<300, more preferably12<A_(T)/A_(M1)<150 and most preferably 15<A_(T)/A_(M1)<80.

The number (N) of rows of holes through which the first portion of thepurge gas is introduced is 1<=N<=5, preferably 1<=N<=3.

The ratio between the tube diameter (D) and the axial separations S1_nof the rows of holes from the sightglass surface is preferably withinthe range of 1<D/S1_n<40, more preferably 1.5<D/S1_n<20 and mostpreferably 1.5<D/S1_n<10.

If separations of holes or rows of holes are specified, these are eachspecified proceeding from the geometric axis of the holes.

For injection of the second portion of the purge gas (M2) at an obliqueangle to the tube axis, preference is given to using rows of holes whichare likewise preferably arranged on the upper side of the tube within anangle range β2_n (n=index for row of holes) of 40°-180°, more preferably50°-130°, most preferably 60°-120°, about the vertical. Rotation of theangle range β2_n including the holes by 0-180° about the tube axis(deviation from the vertical) is possible.

The distance of the holes within a row from the respective neighboringhole may be different or equal within a row, and is preferably equal.

The holes are preferably positioned such that the exit orifices thereofin the sightglass tube are within the angle range β2_n.

All the holes for the second portion of the purge gas (M2) arepreferably aligned parallel to one another and within an angle range αof 10°-80°, more preferably 20°-70°, most preferably 30°-60°, to thetube axis, in the direction of the reactor end of the tube.

The cross-sectional area of the tube (A_(T)) based on the total area(A_(M2)) of all the holes aligned at an oblique angle to the tube axisis preferably 5<A_(T)/A_(M2)<500, more preferably 20<A_(T)/A_(M2)<300and most preferably 40<A_(T)/A_(M2)<150.

The number (K) of rows of holes for the second portion of the purgehydrogen is 1<=K<=5, preferably 1<=K<=3.

The ratio between the tube diameter (D) and the axial separation (S2_k,)of the hole exits (at oblique angles to the tube axis) or rows of holesfrom the sightglass surface is preferably in the range of 0.4<D/S2_k<40,more preferably 0.6<D/S2_k<20 and most preferably (0.8<D/S2_k<10). Sincethe holes run at oblique angles, the distances relative to the geometricaxis of the holes at the holes drilled on the inner surface of the tubeare specified, cf. FIG. 2.

The process according to the invention with its preferred embodimentsvirtually completely suppresses contact between reaction gas from thereactor and the internal glass surface of the sightglass at the reactorend. This completely prevents deposits on the glass surface of thesightglass.

The flow field in the sightglass is independent of the purge gas rate.Therefore, if required, very different purge gas rates can be usedwithout deterioration in the quality of the purging through varying flowconditions.

EXAMPLES

In the tests of the different sightglass types, a standard process witha chlorosilane concentration of 20% (mole fraction) in H₂ was used.

In this process, marked deposits normally form on the reactor walls.

The target diameter of the silicon rods to be deposited was 150 mm.

Comparative Example Tube: L/D=2 and D=50 mm

The sightglass had a row of holes at a distance S1_1 of 10 mm from theglass surface.

The holes were arranged parallel to the glass surface in the upper halfof the sightglass tube and aligned in the direction of the tube axis.

Every 30°, there was a hole of hole diameter 4 mm (7 holes in total). Nofurther purge gas injections were present.

The sightglass was purged with 30 m³ (STP)/h of H₂ through the holes.

During the deposition process, distinctly visible deposits formed on theglass surface at the reactor end in all the batches. These deposits werecomposed of amorphous compounds consisting of: chlorine, silicon andhydrogen.

The deposits distorted the temperature measurements.

The deposition process had to be ended prematurely for all the batcheswithin the rod diameter range of 110-130 mm because of an excessivelyhigh electrical power consumption.

On the basis of the resultant high rod temperatures, increased formationof popcorn was detected.

Example 1 Tube: L/D=2 and D=50 mm.

The sightglass had two mutually offset rows of holes at a distance ofS1_1=15 mm and S1_2=25 mm from the glass surface.

The purge gas mass flow was split into two substreams. The firstsubstream M1 was supplied close to the sightglass, parallel to thesightglass surface.

For this purpose, holes were arranged on the top of the sightglass tubewithin an angle range of β1_1=119° about the zero line (vertical). Theholes were parallel to the glass surface and aligned verticallydownward. The first row consists of 5 holes each with hole diameters of2 mm. The middle hole was on the vertical. Every two further holes werearranged symmetrically to the vertical at a distance of ±10.3 mm or±20.5 mm from the vertical. The second row of holes consisted of fourholes each having hole diameters of 2 [mm], which were arranged offsetfrom the first row of holes at horizontal separations (every two at ±5.1mm and ±15.4 mm) symmetrically to the vertical.

The second portion of the purge gas stream was injected obliquely to thetube axis at an angle of α=30° (angle relative to the tube axis) in thedirection of the reactor through holes parallel to one another. A row offour holes was arranged on the top of the sightglass tube within anangle range of β 2_1=108° about the zero line (vertical). The holes hada diameter of 2 mm. Every two holes were arranged symmetrically to thevertical at a distance of ±9.6 mm or ±19.2 mm from the vertical. Theexit orifices of the holes were at a distance of S2_1=55 mm from theglass surface.

The sightglass was purged with 20 m³ (STP)/h of H₂ through the holes.The ratio of the purge mass flows M1/M2 was 3.

Over the course of the deposition process, no visible deposits formed onthe glass surface at the reactor end in any of the batches.

The deposition process reached the rod diameter of 150 mm in all thebatches. The batches did not have an elevated proportion of popcorn.

Example 2 Tube: L/D=1.3 and D=75 mm

The sightglass had two mutually offset rows of holes at a distance ofS1_1=15 mm and S1_2=25 mm from the glass surface.

The purge gas mass flow was split into two substreams. The firstsubstream M1 was supplied close to the sightglass, parallel to thesightglass surface.

For this purpose, holes were arranged on the top of the sightglass tubewithin an angle range of β1_1=119° about the zero line (vertical). Theholes were parallel to the glass surface and aligned verticallydownward. The first row consists of 7 holes each with hole diameters of3 mm. The middle hole was on the vertical. Every two further holes werearranged symmetrically to the vertical at a distance of ±10.3 mm, ±20.5mm or ±30.8 mm from the vertical. The second row of holes consisted ofsix holes each having hole diameters of 3 [mm], which were arrangedoffset from the first row of holes. Every 2 holes were arranged at adistance of ±5.1 mm, ±15.4 mm and ±25.6 mm symmetrically to thevertical.

The second portion of the purge gas stream was injected obliquely to thetube axis at an angle of α=60° (angle relative to the tube axis) in thedirection of the reactor through holes parallel to one another. A row offour holes was arranged on the top of the sightglass tube within anangle range of β 2_1=65° about the zero line (vertical). The holes had adiameter of 2 mm. Every two holes were arranged symmetrically to thevertical at a distance of ±9.6 mm or ±19.2 mm from the vertical. Theexit orifices of the holes were at a distance of S2_1=65 mm from theglass surface.

The sightglass was purged with 30 m³ (STP)/h of H₂ through the holes.All the purge gas ducts (M1 and M2) were supplied by a common space thatwas fed centrally. The ratio of the purge mass flow rates was calculatedfrom the cross-sectional ratio A_(M1)/A_(M2) and was 7.

Over the course of the deposition process, no visible deposits formed onthe glass surface at the reactor end in any of the batches.

The deposition process reached the rod diameter of 150-160 mm in all thebatches. The morphology of the batches corresponded to thespecification.

While exemplary embodiments are described above, it is not intended thatthese embodiments describe all possible forms of the invention. Rather,the words used in the specification are words of description rather thanlimitation, and it is understood that various changes may be madewithout departing from the spirit and scope of the invention.Additionally, the features of various implementing embodiments may becombined to form further embodiments of the invention.

What is claimed is:
 1. A reactor for producing polycrystalline siliconhaving a reactor wall, comprising: at least one sightglass tube securedto an orifice in the reactor wall at a reactor side end of thesightglass tube and having a sightglass inner surface at the other end,wherein the sightglass tube has a plurality of holes arranged in rows inthe sightglass tube for supplying a purge gas, wherein, a firstplurality of holes are provided for supplying a purge gas stream M1, thefirst plurality of holes positioned at an axial separation S1_n from theinner surface of the sightglass and parallel to the inner surface,wherein a ratio D/S1_n between a sightglass tube inner diameter D andthe axial separation S1_n of a row of holes of the first plurality ofholes from the glass surface is greater than 1 and less than 40, the rowof holes of the first plurality of holes running parallel to the glasssurface, and wherein for supplying at least one further purge gas streamM2 further holes are provided, said further holes being spaced apartfrom the holes running parallel to the glass surface in the direction ofthe reactor-side end of the sightglass, the further plurality of holesrunning at an angle relative to the glass surface in the direction ofthe reactor side end of the sightglass tube.
 2. The reactor of claim 1,wherein a ratio L/D of tube length L to tube diameter D is 0.5-4.0. 3.The reactor of claim 1, wherein the holes in a row of the furtherplurality of holes are each arranged within an angular range β1_n, β2_nof 40°-180° with respect to an internal cross section area of thesightglass tube.
 4. The reactor of claim 1, wherein a ratio D/S2_kbetween the tube diameter D and a maximum axial separation S2_k of a rowof holes of the further plurality of holes from the glass surface isgreater than 0.4 and less than 40, wherein said row of holes comprisesholes that run parallel to each other at an angle with respect to theinner surface in the direction of the reactor side end of the sightglasstube.
 5. The reactor of claim 1, wherein the cross section area of thesightglass tube based on the total cross section area A_(M2) of all theholes provided for supply of purge gas streams M2 is greater than 5 andless than
 500. 6. The reactor of claim 1, wherein the first plurality ofholes and the further plurality of holes are configured as mutuallyoffset rows of holes, each row comprising a plurality of holes.